EP2370194B1 - Rapid static decanter for pre-thickening of sludge from water treatment and installation having said decanter - Google Patents
Rapid static decanter for pre-thickening of sludge from water treatment and installation having said decanter Download PDFInfo
- Publication number
- EP2370194B1 EP2370194B1 EP09801559.7A EP09801559A EP2370194B1 EP 2370194 B1 EP2370194 B1 EP 2370194B1 EP 09801559 A EP09801559 A EP 09801559A EP 2370194 B1 EP2370194 B1 EP 2370194B1
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- EP
- European Patent Office
- Prior art keywords
- sludge
- settler
- concentration
- controlling
- decanter
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- 239000010802 sludge Substances 0.000 title claims description 98
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims description 18
- 230000003068 static effect Effects 0.000 title claims description 7
- 230000008719 thickening Effects 0.000 title description 17
- 238000009434 installation Methods 0.000 title description 4
- 229920000642 polymer Polymers 0.000 claims description 47
- 239000000523 sample Substances 0.000 claims description 28
- 238000000605 extraction Methods 0.000 claims description 20
- 239000007788 liquid Substances 0.000 claims description 20
- 239000007787 solid Substances 0.000 claims description 18
- 238000002347 injection Methods 0.000 claims description 7
- 239000007924 injection Substances 0.000 claims description 7
- 239000002562 thickening agent Substances 0.000 claims description 4
- 230000001737 promoting effect Effects 0.000 claims description 3
- 239000002351 wastewater Substances 0.000 claims description 3
- 230000002093 peripheral effect Effects 0.000 claims description 2
- 230000001105 regulatory effect Effects 0.000 description 11
- 238000012937 correction Methods 0.000 description 10
- 230000004907 flux Effects 0.000 description 9
- 238000005259 measurement Methods 0.000 description 7
- 239000002002 slurry Substances 0.000 description 6
- 239000000243 solution Substances 0.000 description 6
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 4
- 238000011084 recovery Methods 0.000 description 4
- 208000005156 Dehydration Diseases 0.000 description 3
- 230000015556 catabolic process Effects 0.000 description 3
- 230000003247 decreasing effect Effects 0.000 description 3
- 238000006731 degradation reaction Methods 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 229910052698 phosphorus Inorganic materials 0.000 description 3
- 239000011574 phosphorus Substances 0.000 description 3
- 239000000725 suspension Substances 0.000 description 3
- 230000001276 controlling effect Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000005352 clarification Methods 0.000 description 1
- 238000010908 decantation Methods 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 235000021183 entrée Nutrition 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 230000003287 optical effect Effects 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Images
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/01—Separation of suspended solid particles from liquids by sedimentation using flocculating agents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/02—Settling tanks with single outlets for the separated liquid
- B01D21/04—Settling tanks with single outlets for the separated liquid with moving scrapers
- B01D21/06—Settling tanks with single outlets for the separated liquid with moving scrapers with rotating scrapers
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/24—Feed or discharge mechanisms for settling tanks
- B01D21/2405—Feed mechanisms for settling tanks
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/24—Feed or discharge mechanisms for settling tanks
- B01D21/245—Discharge mechanisms for the sediments
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/30—Control equipment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/30—Control equipment
- B01D21/32—Density control of clear liquid or sediment, e.g. optical control ; Control of physical properties
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D21/00—Separation of suspended solid particles from liquids by sedimentation
- B01D21/30—Control equipment
- B01D21/34—Controlling the feed distribution; Controlling the liquid level ; Control of process parameters
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
- B01F35/20—Measuring; Control or regulation
- B01F35/21—Measuring
- B01F35/211—Measuring of the operational parameters
- B01F35/2111—Flow rate
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
- B01F35/20—Measuring; Control or regulation
- B01F35/21—Measuring
- B01F35/211—Measuring of the operational parameters
- B01F35/2111—Flow rate
- B01F35/21111—Mass flow rate
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
- B01F35/20—Measuring; Control or regulation
- B01F35/22—Control or regulation
- B01F35/221—Control or regulation of operational parameters, e.g. level of material in the mixer, temperature or pressure
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
- B01F35/20—Measuring; Control or regulation
- B01F35/22—Control or regulation
- B01F35/221—Control or regulation of operational parameters, e.g. level of material in the mixer, temperature or pressure
- B01F35/2212—Level of the material in the mixer
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
- C02F11/147—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using organic substances
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/008—Control or steering systems not provided for elsewhere in subclass C02F
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5209—Regulation methods for flocculation or precipitation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/10—Solids, e.g. total solids [TS], total suspended solids [TSS] or volatile solids [VS]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/11—Turbidity
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/40—Liquid flow rate
Definitions
- the invention relates to a static decanter for pre-thickening liquid sludge in a water treatment plant, in particular wastewater, having an inclined bottom and equipped with a slurry feed pump, d. a device for injecting polymer into the liquid sludge, an overflow discharge and a pump for extracting pre-thickened sludge from the clarifier.
- Decanters of this type are known, in particular according to Memento Technique of Water, 10th Edition DEGREMONT, Volume 2, pages 833 and following.
- the settling tank is generally downstream of a clarification device, which is located downstream of a ventilation tank.
- the effluent from the clarifier and constituting the liquid sludge entering the decanter has a variable concentration of suspended solids, ranging from 1 to 8 g / l.
- the pre-thickened sludge extracted from the settling tank may have a suspended solids concentration of 15 to 20 g / L.
- the characteristics of the pre-thickened sludge extracted have variations that need to be reduced to optimize the operation of thickening devices installed downstream of the decanter, and to reduce the energy consumption of the assembly.
- the object of the invention is therefore, above all, to provide a static settler which makes it possible to obtain, at the outlet, a pre-thickened sludge favorable to optimum operation of a thickening apparatus, in particular a centrifuge, without causing degradation. the quality of the treated water.
- the invention also aims to provide a decanter equipped to optimize the consumption of polymer.
- the static settling tank is thus a fast settler which makes it possible to obtain pre-thickened sludge in a sufficiently short time to prevent the degradation of the treated water, especially in a time less than that which would lead to a release of phosphorus by the bacteria.
- the released phosphorus would deteriorate the quality of the treated water.
- the fast decanter also ensures a constant and high pre-thickening for the downstream treatment.
- the means for accelerating the decantation of the sludge may comprise an inclination angle of the bottom of the settling tank on the horizontal between 20 ° and 45 °, and a scraper rotating bottom.
- This scraper preferably comprises an arm equipped with scraper blades arranged in ashamedy so as to bring the sludge decanted efficiently and quickly to a central pit. This central pit is also scraped.
- the arm is advantageously equipped with a harrow favoring the pre-thickening of the sludge.
- the scraper arm may be in the shape of a V that follows the bottom of the decanter.
- the means for regulating the concentration of the pre-thickened sludge comprise means for regulating the mass flow of suspended solids entering the decanter, and means for regulating the concentration of the pre-thickened sludge from the mass flow. entering.
- the decanter comprises means for regulating the level of the mud veil suitable for keeping this level as low as possible, with optimization of consumption of the polymer.
- the sludge level regulating means may comprise a mud web height measuring probe, a variable speed polymer feed pump, a flow meter on the polymer injection line, and a regulator or regulator.
- speed variator receiving the information from the sensor measuring the height of the mud web and the flow meter, and able to control the speed of the pump to optimize the consumption of polymer.
- the decanter is designed so that the residence time of the sludge in the decanter does not exceed two hours.
- the decanter comprises a frustoconical bottom section decreasing downwards, the angle of inclination ( ⁇ ) of the generatrices of the bottom on the horizontal being between 20 ° and 45 °.
- the level of the mud web is advantageously maintained substantially at the level of the large base of the frustoconical bottom.
- the peripheral speed of the scraper may be between 10 and 20 cm / s.
- the scraper comprises at least one scraper blade and a harrow.
- the invention also relates to a water treatment plant, characterized in that it comprises a settler as defined above, and in that the extraction outlet of the clarifier is connected directly to a sludge thickening apparatus, in particular a centrifuge or a band filter, without sludge cover between the decanter and the sludge thickener.
- a sludge thickening apparatus in particular a centrifuge or a band filter
- a fast static decanter D for a wastewater treatment plant schematically illustrated on Fig.4 .
- the installation comprises an activated sludge aeration tank 1, followed by a clarifier 2 whose clarified water is extracted in the upper part 2a, while the liquid sludge is directed, in part, to the decanter D, and for the other part are recycled at the head of basin 1.
- the slurry concentration of the liquid sludge entering the decanter D can be from about 1 to 8 g / L.
- the suspended solids concentration of the pre-thickened sludge leaving the decanter D is generally between 15 and 20 g / l.
- the effluent leaving the decanter D is directed to a thickening apparatus, in particular a centrifuge 3.
- the concentration of suspended matter at the outlet of the centrifuge 3 can be between 50 and 60 g / L (or even 200 to 300 g / L).
- the outlet effluent from the centrifuge is sent either to a sludge digestion device 4, to a dehydration apparatus or to a drying device 6.
- the fast settler D is provided to allow the output of pre-thickened sludge having a substantially constant concentration suspended matter, despite variations in concentration at the entrance.
- the fast settler D is constituted by a reactor 7 of vertical axis, with a bottom 8 inclined to the horizontal at an angle ⁇ , which can be between 20 and 45 °.
- the reactor 7 is cylindrical and the bottom 8 is frustoconical, of decreasing section downwards, converge towards a central recovery tank 9.
- the decanter D is equipped with a bottom rotating wiper 10 with a arm 11 in the form of V following, according to the diameter, the bottom 8 of the decanter.
- the arm 11 is equipped with scraper blades 12 arranged in ashamedy ( Fig.2 and 3 ), so as to bring the sludge decanted efficiently and quickly to the central recovery tank 9, also scraped, and a harrow 12a promoting the pre-thickening of the sludge.
- the harrow 12a has vertical blades distributed in the radial direction.
- the central pit 9 is specially designed to avoid short circuits for extracting sludge.
- the decanter D is designed to limit the residence time of the sludge to less than two hours.
- the decanter D is equipped with a variable speed pump 13, for the supply of liquid sludge, which discharges on a discharge line 14 equipped with a probe 15 for measuring the concentration D1 in suspended matter.
- the probe 15 is generally of the optical type.
- a flowmeter 16, in particular of the electromagnetic type, is installed on the pipe 14. Downstream of the flowmeter, a mixer 17 is arranged on the pipe to allow injection into the liquid sludge of polymer promoting the settling of the sludge.
- the injected polymer solution is prepared in a tank B with the addition of drinking water 18.
- a variable speed pump 19 is provided to supply the polymer supply to the mixer 17.
- a flowmeter 20 is installed on the discharge pipe of the pump 19 to provide the polymer solution flow rate sent to the mixer 17.
- the liquid sludge, mixed with the polymer are introduced in the upper part 21 of the settler D which is equipped, in its upper inner part, with a chute 22 to recover the overflow evacuated by an external rejection 23.
- the decanter D is further equipped, in the upper part, with a probe 24 for measuring the height of the veil of sludge V in the decanter.
- the probe 24 is generally of the ultrasonic type.
- Valves 25 are provided at different levels on the outer wall of the decanter to allow sampling.
- the extraction of pre-thickened sludge from the recovery tank 9 is provided by means of a variable speed pump 26, the delivery of which flows into a pipe 27 on which a probe 28 is installed. measuring the concentration D2 in suspended solids and a flow meter 29.
- the feed pump 13 may have a flow rate of between 9 and 53 m 3 / h while the extraction pump 26 may have a flow rate of between 3 and 16 m 3 / h .
- the decanter D can have a diameter of about 3 meters and a height of about 4 meters.
- the information from the probe 15 and the flow meter 16 is sent to a PID regulator 30 whose output controls the speed of rotation of the pump 13.
- the information from the probe 28 and the flowmeter 29 are sent to a PID regulator 31 whose output controls the speed of rotation of the extraction pump 26.
- the information from the probe 24 and the flowmeter 20 is sent to a PID controller, or a variable speed drive, 32 whose output controls the rotational speed of the polymer feed pump 19.
- the regulators 30, 31, with the measurement probes 15, 28, the flow meters 16, 29 and the variable speed pumps 13, 26, constitute means M for regulating the concentration of suspended solids sludge extracted from the decanter D.
- the regulator 30, the measuring probe 15, the flowmeter 16 and the variable speed pump 13 constitute means M1 for controlling the mass flux FM1 of suspended matter entering the decanter D.
- the regulator 31, the measuring probe 28, the flow meter 29 and the variable speed pump 26 constitute means M2 for controlling the concentration of the sludge extracted, from the incoming mass flow FM1.
- the regulator or variator 32, the probe 24 for measuring the height of the veil, the flowmeter 20 and the variable speed pump 19 constitute means M3 for regulating the flow of polymer injected into the decanter D.
- the operation of the decanter D and the control means is as follows.
- the mass flux FM 1 of suspended matter in the water to be treated arriving in the decanter D is fixed by an operator.
- the concentration D1 of suspended solids, in the water to be treated, is delivered by the probe, or sensor, 15.
- F1 be the flow of water to be treated, the mass flow is F1 ⁇ D1 which must be equal to the value fixed FM1.
- the PID regulator 30 sets the speed of the feed pump 13 to maintain the flow setpoint F1 using the measurement of the flowmeter 16.
- the concentration setpoint of the extracted sludge (Cons D2) is set by the operator.
- the flow correction ⁇ Q is plotted on the abscissa and the deviations ⁇ d ConsD2 between the measured value D2 and the setpoint value Cons D2 are plotted on the ordinate.
- the ⁇ Q corrections are positive or negative depending on whether the flow rate should be increased or decreased compared to the flow rate corresponding to point 33.
- the origin of the deviations ⁇ d ConsD2 is located at the value ConsD2, and the deviations are positive when the measurement D2 is greater than ConsD2, and negative in the opposite case.
- the flow correction curves 34, 35 are established experimentally.
- the curve 34 with the steepest slope corresponds to a deconcentration of an effluent with too much solids extracted from the clarifier D
- the curve 35, of lower slope corresponds to a thickening of an effluent that is not sufficiently loaded with solids. Extract from decanter D.
- the reactions of the system are different to deconcentration and thickening, hence the different slopes.
- the first calculated extraction rate F2 gives a concentration value measured by the probe 28 equal to: my D2 which is greater than D2.
- the curve 34 corresponds to the point 36 on the abscissa axis.
- the initial calculated flow rate F2 is increased by ⁇ Q1.
- the regulation provided by the regulator 30 makes it possible to bring the measured concentration closer to the setpoint Cons D2.
- the maximum flow correction values ⁇ ⁇ Q max are of the order of ⁇ 0.5 m 3 / h.
- the measurement signal is an average of 10 minutes, refreshed every minute.
- Fig.6 represents an adjustment curve of the polymer content.
- the level of the mud web is plotted on the ordinate, and the polymer level is plotted on the abscissa.
- the origin Y of the ordinates corresponds to the level of the lowest possible mud web, ie located at the bottom of the decanter D.
- S1 or "Threshold 1" corresponds to the level of the mud web obtained with the polymer content considered as a minimum. This minimum level of polymer may be of the order of 0.5 mg / l.
- S2 or "Threshold 2" corresponds to the level of the sludge haze obtained with the level of polymer considered as maximum. This maximum level may be of the order of 2 mg / L.
- Curve 37 represents the variation of the level of the mud web as a function of the level of polymer to be applied.
- the point E corresponds to the highest possible theoretical level of the web, that is to say at the top at the level of the probe 24; the LSL level, located below "Threshold 1", corresponds to stopping the injection of the polymer.
- the signal indicative of the level of the mud web V is provided by the ultrasonic probe 24. An average of 10 minutes is performed and refreshed every minute.
- the flow rate of the pump 19 remains polymer calculated from the mass flow power calculating FMA calculated. This flow rate is corrected periodically if necessary to maintain the level of the mud V veil in a given range between S1 and S2, and as low as possible. This correction is made under the following conditions.
- the treatment rate T Polym applied to calculate the polymer flow rate will be corrected according to the sludge level measurement taken at the end of the elapsed timer T3.
- the injected polymer content is maintained at the Min. If the level of the veil falls below the LSL Level, the injection is stopped.
- the injected polymer content is maintained at the maximum rate, to lower the mud web.
- the limits of the T Polym applied are for example (0.5 mg / L in min and 2.0 g / L in max.).
- the thresholds S1 and S2 are configurable.
- the invention makes it possible to keep the concentration of the extracted sludge substantially constant and thus to optimize the operation of the machines, in particular centrifuges, downstream of the decanter. This results in a better performance of the installation and a reduction in the energy consumed.
- the invention also makes it possible to reduce the polymer consumption, which is practically halved, while preserving, and even improving, the quality of the extracted sludge.
- the scraper blades 12 of the scraper 10 make it possible to bring the sludge back to zone 9 rapidly in order to reduce their residence time in the decanter D.
- the residence time of the sludge in the decanter is preferably less than 2 hours.
- the harrow 12a makes it possible to set the flocs in motion, favoring degassing and concentrating the sludge.
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Water Supply & Treatment (AREA)
- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Fluid Mechanics (AREA)
- Physics & Mathematics (AREA)
- Centrifugal Separators (AREA)
- Treatment Of Sludge (AREA)
Description
L'invention est relative à un décanteur statique pour pré-épaissir les boues liquides dans une installation de traitement d'eau, en particulier d'eaux usées, comportant un fond incliné et équipé d'une pompe d'alimentation en boues liquides, d'un dispositif d'injection de polymère dans les boues liquides, d'un rejet de surverse et d'une pompe d'extraction des boues pré-épaissies du décanteur.The invention relates to a static decanter for pre-thickening liquid sludge in a water treatment plant, in particular wastewater, having an inclined bottom and equipped with a slurry feed pump, d. a device for injecting polymer into the liquid sludge, an overflow discharge and a pump for extracting pre-thickened sludge from the clarifier.
Des décanteurs de ce type sont connus, notamment d'après le
Dans une installation de traitement d'eau, le décanteur se trouve généralement en aval d'un dispositif de clarification, lequel est situé en aval d'un bassin d'aération. L'effluent provenant du clarificateur et constituant les boues liquides entrant dans le décanteur présente une concentration variable en matières en suspension, pouvant aller de 1 à 8 g/L. Les boues pré-épaissies, extraites du décanteur peuvent présenter une concentration en matières en suspension de 15 à 20 g/L.In a water treatment plant, the settling tank is generally downstream of a clarification device, which is located downstream of a ventilation tank. The effluent from the clarifier and constituting the liquid sludge entering the decanter has a variable concentration of suspended solids, ranging from 1 to 8 g / l. The pre-thickened sludge extracted from the settling tank may have a suspended solids concentration of 15 to 20 g / L.
Ces boues sont ensuite soumises à un traitement d'épaississement ou de déshydratation afin de réduire leur volume.These sludges are then subjected to a thickening or dehydration treatment in order to reduce their volume.
Les caractéristiques des boues pré-épaissies extraites présentent des variations qui demandent à être réduites pour optimiser le fonctionnement des appareils d'épaississement installés en aval du décanteur, et pour diminuer la consommation d'énergie de l'ensemble.The characteristics of the pre-thickened sludge extracted have variations that need to be reduced to optimize the operation of thickening devices installed downstream of the decanter, and to reduce the energy consumption of the assembly.
Il est également souhaitable d'améliorer le degré de pré-épaississement des boues, pour alléger le traitement d'épaississement et de déshydratation, et contribuer ainsi à réduire la consommation d'énergie.It is also desirable to improve the degree of pre-thickening of the sludge, to lighten the thickening and dehydration treatment, and thus contribute to reducing energy consumption.
L'invention a donc pour but, surtout, de fournir un décanteur statique qui permet d'obtenir, en sortie, une boue pré-épaissie favorable à un fonctionnement optimal d'un appareil d'épaississement, notamment une centrifugeuse, sans provoquer une dégradation de la qualité de l'eau traitée.The object of the invention is therefore, above all, to provide a static settler which makes it possible to obtain, at the outlet, a pre-thickened sludge favorable to optimum operation of a thickening apparatus, in particular a centrifuge, without causing degradation. the quality of the treated water.
L'invention a également pour but de fournir un décanteur équipé de manière à optimiser la consommation de polymère.The invention also aims to provide a decanter equipped to optimize the consumption of polymer.
Selon l'invention, un décanteur statique pour pré-épaissir les boues liquides dans une installation de traitement d'eau, en particulier d'eaux usées, en vue d' optimiser le fonctionnement d' appareils d'épaississement installés en aval du décanteur, comporte un fond incliné, est équipé d'une pompe d'alimentation en boues liquides, d'un dispositif d'injection de polymère dans les boues liquides, d'un rejet de surverse et d'une pompe d'extraction des boues pré-épaissies du décanteur,
et est caractérisé en ce qu'il comporte :
- des moyens pour accélérer la décantation des boues,
- des moyens de régulation de la concentration en matières en suspension en sortie des boues pré-épaissies, propres à maintenir sensiblement constante la concentration des boues pré-épaissies extraites du décanteur, malgré les variations de concentrations en entrée,
- et des moyens de régulation du niveau du voile de boue propres à maintenir ce niveau le plus bas possible.
and is characterized in that it comprises:
- means for accelerating the settling of the sludge,
- means for regulating the concentration of suspended solids at the outlet of the pre-thickened sludge, adapted to keep the concentration of the pre-thickened sludge extracted from the clarifier substantially constant, despite the variations in the inlet concentrations,
- and means for regulating the level of the mud web to keep this level as low as possible.
Le décanteur statique est ainsi un décanteur rapide qui permet d'obtenir des boues pré-épaissies en un temps suffisamment court pour éviter la dégradation de l'eau traitée, notamment en un temps inférieur à celui qui entraînerait un relargage du phosphore par les bactéries. Le phosphore relargué détériorerait la qualité de l'eau traitée. Le décanteur rapide assure en outre un pré-épaississement constant et élevé pour le traitement aval.The static settling tank is thus a fast settler which makes it possible to obtain pre-thickened sludge in a sufficiently short time to prevent the degradation of the treated water, especially in a time less than that which would lead to a release of phosphorus by the bacteria. The released phosphorus would deteriorate the quality of the treated water. The fast decanter also ensures a constant and high pre-thickening for the downstream treatment.
Les moyens pour accélérer la décantation des boues peuvent comprendre un angle d'inclinaison du fond du décanteur sur l'horizontale compris entre 20°et 45°, ainsi qu'un racleur tournant de fond. Ce racleur comporte de préférence un bras équipé de lames racleuses disposées en jalousie de manière à ramener efficacement et rapidement les boues décantées vers une fosse centrale. Cette fosse centrale est aussi raclée. Le bras est avantageusement équipé d'une herse favorisant le pré-épaississement de la boue. Le bras du racleur peut avoir la forme d'un V épousant le fond du décanteur.The means for accelerating the decantation of the sludge may comprise an inclination angle of the bottom of the settling tank on the horizontal between 20 ° and 45 °, and a scraper rotating bottom. This scraper preferably comprises an arm equipped with scraper blades arranged in jealousy so as to bring the sludge decanted efficiently and quickly to a central pit. This central pit is also scraped. The arm is advantageously equipped with a harrow favoring the pre-thickening of the sludge. The scraper arm may be in the shape of a V that follows the bottom of the decanter.
De préférence, les moyens de régulation de la concentration des boues pré-épaissies comprennent des moyens de régulation du flux massique de matières en suspension entrant dans le décanteur, et des moyens de régulation de la concentration des boues pré-épaissies à partir du flux massique entrant.Preferably, the means for regulating the concentration of the pre-thickened sludge comprise means for regulating the mass flow of suspended solids entering the decanter, and means for regulating the concentration of the pre-thickened sludge from the mass flow. entering.
Avantageusement, les moyens de régulation du flux massique de matières en suspension entrant dans le décanteur comprennent :
- une pompe d'alimentation en boues liquides à vitesse variable,
- un débitmètre de boues liquides,
- une sonde de mesure de la concentration de matières en suspension dans les boues liquides, et
- un régulateur qui reçoit les informations provenant du débitmètre et de la sonde, et commande la vitesse de la pompe d'alimentation pour maintenir sensiblement constant le flux massique d'alimentation.
- a slurry feed pump with variable speed,
- a flowmeter of liquid sludge,
- a probe for measuring the concentration of suspended solids in liquid sludge, and
- a controller that receives the information from the flow meter and the probe, and controls the speed of the feed pump to keep the feed mass flow substantially constant.
De préférence, les moyens de régulation de la concentration des boues pré-épaissies à partir du flux massique entrant comprennent :
- une pompe d'extraction des boues pré-épaissies à vitesse variable,
- un débitmètre de boues pré-épaissies,
- une sonde de mesure de la concentration de matières en suspension dans les boues pré-épaissies, et
- un régulateur qui reçoit les informations provenant du débitmètre et de la sonde, et commande la vitesse de la pompe d'extraction pour maintenir sensiblement constante la concentration des boues pré-épaissies extraites, le débit d'extraction initial étant calculé à partir du flux massique entrant et d'une consigne de concentration de la boue pré-épaissie extraite.
- a pre-thickened sludge extraction pump with variable speed,
- a flowmeter of pre-thickened sludge,
- a probe for measuring the concentration of suspended solids in the pre-thickened sludge, and
- a regulator which receives the information from the flowmeter and the probe, and controls the speed of the extraction pump to keep the concentration of the pre-thickened sludge extracted substantially constant, the initial extraction rate being calculated from the mass flow entering and a concentration setpoint of the pre-thickened mud extracted.
Avantageusement, le décanteur comporte des moyens de régulation du niveau du voile de boue propres à maintenir ce niveau le plus bas possible, avec optimisation de consommation du polymère.Advantageously, the decanter comprises means for regulating the level of the mud veil suitable for keeping this level as low as possible, with optimization of consumption of the polymer.
Les moyens de régulation du niveau du voile de boue peuvent comprendre une sonde de mesure de la hauteur du voile de boue, une pompe d'alimentation en polymère à vitesse variable, un débitmètre sur la conduite d'injection du polymère, et un régulateur ou variateur de vitesse recevant les informations de la sonde de mesure de la hauteur du voile de boue et du débitmètre, et propre à commander la vitesse de la pompe pour optimiser la consommation de polymère.The sludge level regulating means may comprise a mud web height measuring probe, a variable speed polymer feed pump, a flow meter on the polymer injection line, and a regulator or regulator. speed variator receiving the information from the sensor measuring the height of the mud web and the flow meter, and able to control the speed of the pump to optimize the consumption of polymer.
Le décanteur est prévu pour que le temps de séjour de la boue dans le décanteur ne dépasse pas deux heures. De préférence, le décanteur comporte un fond tronconique de section décroissante vers le bas, l'angle d'inclinaison (α) des génératrices du fond sur l'horizontale étant compris entre 20° et 45°. Le niveau du voile de boue est avantageusement maintenu sensiblement au niveau de la grande base du fond tronconique. La vitesse périphérique du racleur peut être comprise entre 10 et 20 cm/s. Avantageusement, le racleur comprend au moins une lame racleuse et une herse.The decanter is designed so that the residence time of the sludge in the decanter does not exceed two hours. Preferably, the decanter comprises a frustoconical bottom section decreasing downwards, the angle of inclination (α) of the generatrices of the bottom on the horizontal being between 20 ° and 45 °. The level of the mud web is advantageously maintained substantially at the level of the large base of the frustoconical bottom. The peripheral speed of the scraper may be between 10 and 20 cm / s. Advantageously, the scraper comprises at least one scraper blade and a harrow.
L'invention concerne également une installation de traitement d'eau, caractérisée en ce qu'elle comporte un décanteur tel que défini précédemment, et en ce que la sortie d'extraction du décanteur est reliée directement à un appareil d'épaississement des boues, en particulier une centrifugeuse ou un filtre à bande, sans bâche tampon de boue entre le décanteur et l'appareil d'épaississement de boues.The invention also relates to a water treatment plant, characterized in that it comprises a settler as defined above, and in that the extraction outlet of the clarifier is connected directly to a sludge thickening apparatus, in particular a centrifuge or a band filter, without sludge cover between the decanter and the sludge thickener.
L'invention consiste, mises à part les dispositions exposées ci-dessus, en un certain nombre d'autres dispositions dont il sera plus explicitement question ci-après à propos d'un exemple de réalisation décrit avec référence aux dessins annexés, mais qui n'est nullement limitatif. Sur ces dessins :
-
Fig. 1 est une coupe verticale schématique d'un décanteur selon l'invention, avec ses équipements. -
Fig. 2 est une coupe verticale diamétrale, à plus grande échelle, montrant des détails du racleur tournant avec ses lames racleuses et sa herse. -
Fig.3 est une coupe horizontale schématique du racleur deFig.2 . -
Fig.4 est un schéma sommaire d'une installation de traitement d'eau avec décanteur selon l'invention. -
Fig. 5 est un diagramme illustrant la correction de l'ajustement du débit d'extraction, et -
Fig.6 est un diagramme illustrant le principe du calcul du taux de polymère appliqué.
-
Fig. 1 is a schematic vertical section of a decanter according to the invention, with its equipment. -
Fig. 2 is a diametrical vertical section, on a larger scale, showing details of the scraper rotating with its scraper blades and its harrow. -
Fig.3 is a schematic horizontal section of the scraperFig.2 . -
Fig.4 is a summary diagram of a water treatment plant with settler according to the invention. -
Fig. 5 is a diagram illustrating the correction of the adjustment of the extraction rate, and -
Fig.6 is a diagram illustrating the principle of calculation of the applied polymer level.
En se reportant à
La concentration en matières en suspension des boues liquides qui arrivent dans le décanteur D peut être d'environ 1à 8 g/L. La concentration en matières en suspension de la boue pré-épaissie sortant du décanteur D est généralement comprise entre 15 et 20 g/L. L'effluent sortant du décanteur D est dirigé vers un appareil d'épaississement, notamment une centrifugeuse 3. La concentration en matières en suspension à la sortie de la centrifugeuse 3 peut être comprise entre 50 et 60 g/L (voire de 200 à 300 g/L). L'effluent de sortie de la centrifugeuse est envoyé soit à un dispositif 4 de digestion des boues, soit à un appareil 5 de déshydratation, soit à un dispositif 6 de séchage.The slurry concentration of the liquid sludge entering the decanter D can be from about 1 to 8 g / L. The suspended solids concentration of the pre-thickened sludge leaving the decanter D is generally between 15 and 20 g / l. The effluent leaving the decanter D is directed to a thickening apparatus, in particular a centrifuge 3. The concentration of suspended matter at the outlet of the centrifuge 3 can be between 50 and 60 g / L (or even 200 to 300 g / L). The outlet effluent from the centrifuge is sent either to a sludge digestion device 4, to a dehydration apparatus or to a drying device 6.
Afin de faire fonctionner à l'optimum de ses performances l'appareil d'épaississement, notamment la centrifugeuse 3, le décanteur rapide D selon l'invention est prévu pour permettre d'obtenir en sortie une boue pré-épaissie ayant une concentration sensiblement constante en matières en suspension, malgré les variations de concentration à l'entrée.In order to operate at optimum performance the thickening apparatus, in particular the centrifuge 3, the fast settler D according to the invention is provided to allow the output of pre-thickened sludge having a substantially constant concentration suspended matter, despite variations in concentration at the entrance.
Comme visible sur
Généralement, le réacteur 7 est cylindrique et le fond 8 est tronconique, de section décroissante vers le bas, convergent vers une fosse centrale de récupération 9. Le décanteur D est équipé d'un racleur tournant 10 de fond avec un bras 11 en forme de V épousant, suivant le diamètre, le fond 8 du décanteur. Le bras 11 est équipé de lames racleuses 12 disposées en jalousie (
Le décanteur D est équipé d'une pompe 13 à vitesse variable, pour l'alimentation en boues liquides, qui débite sur une conduite de refoulement 14 équipée d'une sonde 15 de mesure de la concentration D1 en matières en suspension. La sonde 15 est généralement du type optique. Un débitmètre 16, notamment de type électromagnétique, est installé sur la conduite 14. En aval du débitmètre un mélangeur 17 est disposé sur la conduite pour permettre l'injection dans la boue liquide de polymère favorisant la décantation des boues. La solution de polymère injectée est préparée dans une cuve B avec addition d'eau potable 18. Une pompe à vitesse variable 19 est prévue pour assurer l'alimentation en polymère du mélangeur 17. Un débitmètre 20 est installé sur la conduite de refoulement de la pompe 19 pour fournir le débit de solution de polymère envoyé au mélangeur 17. Les boues liquides, mélangées avec le polymère, sont introduites en partie haute 21 du décanteur D qui est équipé, dans sa partie supérieure intérieure, d'une goulotte 22 pour récupérer la surverse évacuée par un rejet 23 extérieur.The decanter D is equipped with a
Le décanteur D est en outre équipé, en partie haute, d'une sonde 24 de mesure de la hauteur du voile de boue V dans le décanteur. La sonde 24 est généralement du type à ultrasons. Des vannes 25 sont prévues à différents niveaux sur la paroi extérieure du décanteur pour permettre des prises d'échantillons.The decanter D is further equipped, in the upper part, with a
L'extraction des boues pré-épaissies, à partir de la fosse 9 de récupération, est assurée à l'aide d'une pompe à vitesse variable 26 dont le refoulement débite dans une conduite 27 sur laquelle est installée une sonde 28 de mesure de la concentration D2 en matières en suspension et un débitmètre 29.The extraction of pre-thickened sludge from the recovery tank 9 is provided by means of a
A titre d'exemples numériques, non limitatifs, la pompe d'alimentation 13 peut avoir un débit compris entre 9 et 53 m3/h tandis que la pompe d'extraction 26 peut avoir un débit compris entre 3 et 16 m3/h. Le décanteur D peut avoir un diamètre d'environ 3 mètres et une hauteur d'environ 4 mètres.As numerical examples, non-limiting, the
Les informations provenant de la sonde 15 et du débitmètre 16 sont envoyées à un régulateur PID 30 dont la sortie commande la vitesse de rotation de la pompe 13.The information from the
Les informations provenant de la sonde 28 et du débitmètre 29 sont envoyées sur un régulateur PID 31 dont la sortie commande la vitesse de rotation de la pompe d'extraction 26.The information from the
Les informations provenant de la sonde 24 et du débitmètre 20 sont envoyées sur un régulateur PID, ou un variateur de vitesse, 32 dont la sortie commande la vitesse de rotation de la pompe 19 d'alimentation en polymère.The information from the
Les régulateurs 30, 31, avec les sondes de mesure 15, 28, les débitmètres 16, 29 et les pompes à vitesse variable 13, 26, constituent des moyens M de régulation de la concentration en matières en suspension des boues extraites du décanteur D.The
Le régulateur 30, la sonde de mesure 15, le débitmètre 16 et la pompe à vitesse variable 13 constituent des moyens M1 de régulation du flux massique FM1 de matières en suspension entrant dans le décanteur D.The
Le régulateur 31, la sonde de mesure 28, le débitmètre 29 et la pompe à vitesse variable 26 constituent des moyens M2 de régulation de la concentration des boues extraites, à partir du flux massique entrant FM1.The
Le régulateur ou variateur 32, la sonde 24 de mesure de la hauteur du voile, le débitmètre 20 et la pompe à vitesse variable 19 constituent des moyens M3 de régulation du débit de polymère injecté dans le décanteur D.The regulator or
L'automatisme de pilotage des flux traités sur le décanteur D repose sur ces différentes régulations :
- le contrôle du flux constant FM1 d'alimentation en boue liquide du réacteur,
- le contrôle du maintien de la concentration D2 des boues extraites pré-épaissies,
- le maintien au plus bas du niveau du voile V de boue dans le réacteur D avec une optimisation de la consommation du polymère.
- the control of the constant flow flux FM1 liquid slurry reactor,
- the control of the maintenance of the D2 concentration of the pre-thickened extracted sludge,
- keeping the level of the veil M of the slurry in the reactor D at a low level with optimization of the consumption of the polymer.
L'ensemble de ces trois régulations permet d'assurer :
- l'optimisation de la consommation du polymère injecté, dés que la nécessité d'ajouter le polymère apparaît ;
- la surveillance de la qualité de l'eau clarifiée en surverse.
- le maintien du voile de boue à un niveau le plus faible possible pour éviter des temps de séjour élevés, un vieillissement et une dégradation de la boue pré-épaissie (dénitrification des boues, relargage du phosphore).
- le maintien de la concentration constante des boues de sortie, ce qui permet de réduire, voire de supprimer, une bâche tampon de récupération des boues pré-épaissies, habituellement placée en amont de la centrifugeuse 3 et en aval du décanteur D.
- optimizing the consumption of the injected polymer, as soon as the need to add the polymer appears;
- monitoring the quality of clarified water overflow.
- keeping the mud web as low as possible to avoid high residence times, aging and degradation of the pre-thickened sludge (denitrification of sludge, release of phosphorus).
- maintaining the constant concentration of the sludge, which makes it possible to reduce, or even eliminate, a pre-thickened sludge recovery pad, usually placed upstream of the centrifuge 3 and downstream of the settler D.
Le fonctionnement du décanteur D et des moyens de régulation est le suivant.The operation of the decanter D and the control means is as follows.
Le flux massique FM 1 de matières en suspension dans l'eau à traiter arrivant dans le décanteur D est fixé par un opérateur. La concentration D1 de matières en suspension, dans l'eau à traiter, est délivrée par la sonde, ou capteur, 15. Soit F1 le débit d'eau à traiter, le flux massique est F1×D1 qui doit être égal à la valeur fixée FM1. La consigne de débit F1 à assurer est déterminée par :
Le régulateur PID 30 positionne la vitesse de la pompe d'alimentation 13 pour maintenir la consigne de débit F1 en utilisant la mesure du débitmètre 16.The
La consigne de concentration de la boue extraite (Cons D2) est fixée par l'opérateur. Un premier débit d'extraction F2 est calculé en supposant en première approximation que la concentration effective de la boue extraite est égale à la valeur choisie de consigne. Dans ce cas, en écrivant que le flux massique extrait est égal au flux massique entrant : F2x Cons D2 = FM 1, on déduit :
Le régulateur PID 31 positionne la vitesse de la pompe d'extraction 26 pour maintenir la consigne de débit Q = F2, en utilisant la mesure du débitmètre 29. Toutefois, la concentration D2 de la boue extraite, mesurée par la sonde 27, ne sera pas égale à Cons D2, mais en sera voisine. Une correction périodique (toutes les 30secondes à 300secondes) de débit est effectuée pour ajuster le débit afin d'obtenir une concentration de sortie égale à la consigne fixée.The
Cette correction de débit est expliquée avec référence au diagramme de
Dans l'exemple illustré sur
Dans la pratique les valeurs maximales de correction de débit ± ΔQ maxi sont de l'ordre de ± 0.5 m3/h. Le signal de mesure correspond à une moyenne sur 10 minutes, rafraîchie toutes les minutes.In practice the maximum flow correction values ± ΔQ max are of the order of ± 0.5 m 3 / h. The measurement signal is an average of 10 minutes, refreshed every minute.
La pompe 19 de polymère est pilotée par le régulateur 32 ou variateur de vitesse, et la consigne de vitesse est calculée à partir du flux massique d'alimentation FM1 = F1×D1 et de la position du niveau de voile de boue V.The
La consigne de polymère est calculée avec les éléments suivants :
- TPolym = Taux de traitement de polymère (dose optimale de polymère à injecter dans l'eau à traiter)
- CPolym = concentration du polymère (concentration du polymère dans la solution injectée)
- Cons Qpolym =Consigne du débit de polymère (consigne du débit de la solution de polymère injectée)
- d'où la consigne de débit de polymère :
- T Polym = Polymer treatment rate ( optimal dose of polymer to be injected into the water to be treated )
- C Polym = concentration of the polymer ( concentration of the polymer in the injected solution )
- Cons Q polym = Polymer flow rate setpoint ( flow rate of the injected polymer solution )
- hence the polymer flow setpoint:
Les explications qui suivent sont données avec référence à
L'origine O des ordonnées correspond au niveau de voile de boue le plus bas possible, c'est à dire situé au fond du décanteur D. S1 ou « Seuil 1 » correspond au niveau du voile de boue obtenu avec le taux de polymère considéré comme minimum. Ce taux mini de polymère peut être de l'ordre de 0.5 mg/L. S2 ou « Seuil 2 » correspond au niveau du voile de boue obtenu avec le taux de polymère considéré comme maximum. Ce taux maxi peut être de l'ordre de 2 mg/L. La courbe 37 représente la variation du niveau du voile de boue en fonction du taux de polymère à appliquer.The origin Y of the ordinates corresponds to the level of the lowest possible mud web, ie located at the bottom of the decanter D. S1 or "
Sur l'axe des ordonnées, le point E correspond au niveau théorique le plus haut possible du voile, c'est-à-dire au sommet au niveau de la sonde 24 ; le point Niveau LSL, situé au-dessous de « Seuil 1 » correspond à l'arrêt de l'injection du polymère.On the ordinate axis, the point E corresponds to the highest possible theoretical level of the web, that is to say at the top at the level of the
Le signal indiquant le niveau du voile de boue V est fourni par la sonde 24 à ultrasons. Une moyenne sur 10mn est effectuée et rafraîchie toutes les minutes.The signal indicative of the level of the mud web V is provided by the
Le débit de la pompe 19 de polymère reste calculé à partir du flux massique d'alimentation calculé FMA calculé. Ce débit est corrigé périodiquement si nécessaire pour maintenir le niveau du voile de boue V dans une plage donnée comprise entre S1 et S2, et le plus bas possible. Cette correction est effectuée dans les conditions suivantes.The flow rate of the
Périodiquement toutes les T3 secondes, avec 1s < T3 < 1800 s, la position du voile du niveau du voile de boue V est surveillée. Au « Niveau (t) », à l'instant t correspond le « taux appliqué ».Periodically every T3 seconds, with 1s <T3 <1800 s, the position of the veil of the level of the mud veil V is monitored. At "Level (t)", at time t corresponds the "applied rate".
Le taux de traitement TPolym appliqué pour calculer le débit de polymère sera corrigé en fonction de la mesure de niveau du voile de boue pris à la fin de la temporisation T3 écoulée.The treatment rate T Polym applied to calculate the polymer flow rate will be corrected according to the sludge level measurement taken at the end of the elapsed timer T3.
Tant que « Niveau(t) » reste dans la fourchette comprise entre S1 et S2, le taux de polymère appliqué est ajusté, conformément à la portion de droite 37.As long as "Level (t)" remains in the range between S1 and S2, the applied polymer level is adjusted, according to the
Dés que le niveau du voile de boue devient inférieur au seuil S1, le taux de polymère injecté est maintenu au Taux mini. Si le niveau du voile descend en dessous du Niveau LSL, l'injection est arrêtée.As soon as the sludge level falls below the threshold S1, the injected polymer content is maintained at the Min. If the level of the veil falls below the LSL Level, the injection is stopped.
Lorsque le niveau du voile de boue devient supérieur au seuil S2, le taux de polymère injecté est maintenu au Taux maxi, pour faire descendre le voile de boue.When the level of the mud web becomes greater than the threshold S2, the injected polymer content is maintained at the maximum rate, to lower the mud web.
Les limites du TPolym appliqué sont par exemple (0,5 mg/L en mini et 2,0 g/L en maxi.). Au démarrage le premier calcul se fait avec un taux initial (T init Polym) paramétrable. Les seuils S1 et S2 sont paramétrables.The limits of the T Polym applied are for example (0.5 mg / L in min and 2.0 g / L in max.). At startup the first calculation is done with an initial rate (T init Polym ) parameterizable. The thresholds S1 and S2 are configurable.
L'invention permet de maintenir sensiblement constante la concentration des boues extraites et d'optimiser ainsi le fonctionnement des machines, notamment centrifugeuses, en aval du décanteur. Il en résulte un meilleur rendement de l'installation et une diminution de l'énergie consommée.The invention makes it possible to keep the concentration of the extracted sludge substantially constant and thus to optimize the operation of the machines, in particular centrifuges, downstream of the decanter. This results in a better performance of the installation and a reduction in the energy consumed.
L'invention permet également de réduire la consommation de polymère, qui est divisée pratiquement par deux, tout en conservant, et même améliorant, la qualité des boues extraites.The invention also makes it possible to reduce the polymer consumption, which is practically halved, while preserving, and even improving, the quality of the extracted sludge.
Les lames racleuses 12 du racleur 10 permettent de ramener rapidement les boues vers la zone 9 pour diminuer leur temps de séjour dans le décanteur D. Le temps de séjour des boues dans le décanteur est de préférence inférieur à 2 heures.The
La herse 12a permet de mettre en mouvement les flocs, favorisant un dégazage et une concentration des boues.The
Claims (9)
- A static settler for prethickening liquid sludge in a water treatment plant, in particular a wastewater plant, for optimizing the operation of the thickeners installed downstream of the settler, and, for providing that the residence time of the sludge in the settler does not exceed two hours, being equipped with- a liquid sludge feed pump (13),- a device (17) for injecting polymer into the liquid sludge,- an overflow discharge (23)- a pump (26) for extracting the prethickened sludge from the settler,- means for accelerating the settling of the sludge comprising an inclined bottom (8) of the settler,- means (M) for controlling the suspended solids concentration of the prethickened sludge at the outlet, capable of maintaining the concentration of the prethickened sludge extracted from the settler substantially constant, despite concentration variations at the inlet, and comprising means (M1) for controlling the mass flow (FM1) of suspended solids entering the settler, and means (M2) for controlling the concentration of the prethickened sludge from the inlet mass flow,and means (M3) for controlling the level of the sludge blanket (V) capable of maintaining said level as low as possible, the means (M3) for controlling the level of the sludge blanket comprising a probe (24) for measuring the height of the sludge blanket, a variable speed polymer feed pump (19), a flowmeter (20) on the polymer injection line, and a controller (32) or speed variator receiving the data from the probe (24) measuring the height of the sludge blanket and from the flowmeter (20), and capable of controlling the speed of the pump (19) to optimize the polymer consumption.
- The settler as claimed in claim 1, characterized in that the means for accelerating the settling of the sludge comprise an angle of inclination (a) of the bottom (8) of the settler to the horizontal of between 20° and 45°, and a rotating bottom scraper (10).
- The settler as claimed in claim 2, characterized in that the scraper (10) comprises an arm (11) equipped with scraper blades (12) disposed in a slatted arrangement so as to convey the settled sludge effectively and rapidly toward a central pit (9) which is also scraped.
- The settler as claimed in claim 3, characterized in that the arm (11) is equipped with a harrow (12a) promoting the prethickening of the sludge.
- The settler as claimed in any one of the preceding claims, characterized in that the means (M1) for controlling the mass flow of suspended solids entering the settler comprise:- a variable speed liquid sludge feed pump (13),- a liquid sludge flowmeter (16),- a probe (15) for measuring the suspended solids concentration (D1) of the liquid sludge, and- a controller (30) capable of receiving the data from the flowmeter (16) and from the probe (15), and capable of controlling the speed of the feed pump (13) to maintain the feed mass flow (FM1) substantially constant.
- The settler as claimed in any one of the preceding claims, characterized in that the means (M2) for controlling the concentration of the extracted sludge from the inlet mass flow comprise:- a variable speed prethickened sludge extraction pump (26),- a prethickened sludge flowmeter (29),- a probe (28) for measuring the suspended solids concentration (D2) of the prethickened sludge, and- a controller (31) capable of receiving the data from the flowmeter (29) and from the probe (28), and capable of controlling the speed of the extraction pump (26) to maintain the concentration of prethickened sludge substantially constant, the initial extraction rate being calculated from the inlet mass flow (FM1) and an extracted sludge concentration setpoint (Stpt D2).
- The settler as claimed in any one of the preceding claims, characterized in that the level of the sludge blanket (V) can be maintained substantially at the level of the large base of the frustoconical bottom by the controlling means.
- The settler as claimed in claim 2, characterized in that the peripheral speed of the scraper (10) is between 10 and 20 cm/s.
- A water treatment plant, characterized in that it comprises a settler as claimed in any one of the preceding claims, and in that the settler extraction outlet is connected directly to a sludge thickener, in particular a centrifuge (3) or a belt filter, without a thickened sludge buffer tank between the settler (D) and the sludge thickener.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0807445A FR2940270B1 (en) | 2008-12-24 | 2008-12-24 | RAPID STATIC DECANTER FOR PRE-THICKENING WATER TREATMENT SLUDGE, AND INSTALLATION COMPRISING SUCH DECANTER. |
PCT/IB2009/055928 WO2010073222A1 (en) | 2008-12-24 | 2009-12-23 | Quick static decanter for prethickening water treatment sludge, and plant including such a decanter |
Publications (2)
Publication Number | Publication Date |
---|---|
EP2370194A1 EP2370194A1 (en) | 2011-10-05 |
EP2370194B1 true EP2370194B1 (en) | 2019-04-10 |
Family
ID=41066348
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP09801559.7A Active EP2370194B1 (en) | 2008-12-24 | 2009-12-23 | Rapid static decanter for pre-thickening of sludge from water treatment and installation having said decanter |
Country Status (10)
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---|---|
US (1) | US9011677B2 (en) |
EP (1) | EP2370194B1 (en) |
CN (1) | CN102264445B (en) |
BR (1) | BRPI0923619A2 (en) |
CA (1) | CA2750849C (en) |
ES (1) | ES2733877T3 (en) |
FR (1) | FR2940270B1 (en) |
PT (1) | PT2370194T (en) |
RU (1) | RU2501742C2 (en) |
WO (1) | WO2010073222A1 (en) |
Families Citing this family (14)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2012135696A2 (en) * | 2011-04-01 | 2012-10-04 | University Of South Alabama | Methods and compositions for the diagnosis, classification, and treatment of cancer |
FR3000054B1 (en) * | 2012-12-26 | 2017-11-03 | Degremont | PROCESS FOR TREATING PRIMARY MUNICIPAL OR INDUSTRIAL WASTEWATER SLUDGES AND INSTALLATION FOR CARRYING OUT SAID METHOD |
JP5900576B1 (en) * | 2014-10-24 | 2016-04-06 | 栗田工業株式会社 | Water treatment method and water treatment apparatus |
FR3040388B1 (en) * | 2015-08-27 | 2022-02-11 | Degremont | WASTEWATER TREATMENT PROCESS COMPRISING A RAPID STATIC DECANTER AND ASSOCIATED INSTALLATION |
JP6269635B2 (en) * | 2015-11-02 | 2018-01-31 | 栗田工業株式会社 | Precipitation tank and its operation method |
CN106362606A (en) * | 2016-10-18 | 2017-02-01 | 上海锅炉厂有限公司 | Device and method for producing magnetic suspension |
GB2560153B8 (en) | 2017-01-30 | 2021-01-13 | Intellisense Io Ltd | Mineral recovery control |
US11873238B2 (en) | 2017-01-30 | 2024-01-16 | Intellisense.Io Ltd | Mineral recovery control |
JP6875166B2 (en) * | 2017-03-27 | 2021-05-19 | 住友重機械エンバイロメント株式会社 | Coagulation sedimentation processing equipment |
CA3066213A1 (en) * | 2017-06-07 | 2018-12-13 | Kadant Black Clawson Llc | Improved clarifier with independent sump scraper drive |
DE102017126251A1 (en) * | 2017-11-09 | 2019-05-09 | Huber Se | Wastewater treatment plant and process for the treatment of wastewater |
CN107854872A (en) * | 2017-12-11 | 2018-03-30 | 北京北排装备产业有限公司 | A kind of nonmetallic chain-type mud scraper underwater monitoring device and its application method |
JP7056825B2 (en) * | 2018-03-13 | 2022-04-19 | 住友重機械エンバイロメント株式会社 | Solid-liquid separator |
CN109534414A (en) * | 2018-11-29 | 2019-03-29 | 泰禹丰机械制造(信阳)有限公司 | A kind of effective equipment for intercepting removing jellyfish |
Family Cites Families (34)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US1518136A (en) | 1922-04-25 | 1924-12-09 | Dorr Co | Automatic density control for thickeners |
US2154132A (en) * | 1936-05-28 | 1939-04-11 | Edward B Mallory | Process of controlling the purification of sewage |
US2365293A (en) * | 1941-04-25 | 1944-12-19 | Worthington Pump & Mach Corp | Water treating apparatus |
US3281594A (en) | 1959-08-28 | 1966-10-25 | Walter E Garrison | Sludge-pumping control system |
US3608723A (en) * | 1968-12-05 | 1971-09-28 | Met Pro Water Treatment Corp | Floc blanket level controller comprising means for sensing light diffusely reflected from the floc blanket |
DE1911007B2 (en) * | 1969-03-04 | 1980-04-17 | Passavant-Werke Michelbacher Huette, 6209 Aarbergen | Device for gravity thickening of sludge |
ZA766411B (en) * | 1975-11-10 | 1977-10-26 | American Minechem Corp | Method and apparatus for controlled dewaterizing of coal treatment underflow |
NL7614571A (en) * | 1976-01-02 | 1977-07-05 | I U Conversion Systems Inc | ESTABLISHMENT AND METHOD FOR THICKING SLUDGE. |
US4055494A (en) | 1977-02-14 | 1977-10-25 | Envirotech Corporation | Thickening device and method |
US4226714A (en) * | 1978-12-27 | 1980-10-07 | The Anaconda Company | Thickener control system |
US4392955A (en) * | 1979-12-26 | 1983-07-12 | Ecodyne Corporation | Liquid treatment apparatus |
SU874102A1 (en) * | 1980-02-22 | 1981-10-23 | Предприятие П/Я Р-6956 | Decanting vessel |
AT381691B (en) * | 1982-01-07 | 1986-11-10 | Andritz Ag Maschf | METHOD FOR CONTROLLING A DRAINAGE MACHINE AND DRAINAGE MACHINE |
ATE39679T1 (en) * | 1983-11-28 | 1989-01-15 | Mueller Johann Ag Kieswerk | TANK AND PLANT FOR CLEANING LIQUIDS LOADED WITH SOLIDS. |
JPH07121327B2 (en) * | 1985-11-22 | 1995-12-25 | 株式会社安川電機 | Management method of sludge concentration meter in gravity sludge thickener |
US5006231A (en) * | 1989-03-20 | 1991-04-09 | Consolidation Coal Company | Flocculant control system |
CA2019262A1 (en) * | 1989-06-20 | 1990-12-20 | Ian Christopher Robertson Gilchrist | Sedimentation control process |
DE4138469A1 (en) * | 1991-11-22 | 1993-05-27 | Intersepara Holding Ag Huenenb | Suspension purificn. and pre-thickening - has inflow set according to outflow for max efficiency at a following discontinuous filter press |
US5435924A (en) * | 1994-02-16 | 1995-07-25 | Albertson; Orris E. | Sludge collection apparatus and method |
US5601704A (en) * | 1994-04-11 | 1997-02-11 | The Graver Company | Automatic feedback control system for a water treatment apparatus |
AU3064897A (en) * | 1996-05-16 | 1997-12-05 | Baker Hughes Incorporated | Method and apparatus for controlling thickeners, clarifiers and settling tanks |
US5904855A (en) * | 1997-02-27 | 1999-05-18 | David H. Manz | Closed chemically enhanced treatment system |
FR2767143A1 (en) * | 1997-08-06 | 1999-02-12 | Le Nickel Sln | Method for diminishing water content of nickel iron oxide pulp |
JP3836250B2 (en) * | 1998-05-08 | 2006-10-25 | オルガノ株式会社 | Coagulation sedimentation equipment |
FR2784093B1 (en) * | 1998-10-06 | 2000-11-24 | Suez Lyonnaise Des Eaux | IMPROVEMENTS TO WASTEWATER TREATMENT ACCORDING TO ACTIVATED SLUDGE PROCESSES |
SE9901772D0 (en) * | 1999-05-14 | 1999-05-14 | Sven Bernhardsson | process |
US6408227B1 (en) * | 1999-09-29 | 2002-06-18 | The University Of Iowa Research Foundation | System and method for controlling effluents in treatment systems |
US6673240B2 (en) * | 2001-03-16 | 2004-01-06 | John J. Fassbender | Feed control system for liquid clarification tanks |
DE10148474A1 (en) * | 2001-10-01 | 2003-05-08 | Koehler August Papierfab | Process and device for cleaning waste water |
US6673246B2 (en) * | 2002-02-28 | 2004-01-06 | The United States Of America As Represented By The Secretary Of The Navy | Reusable polysilsesquioxane adsorbents for pollutants |
US6814874B2 (en) * | 2002-08-06 | 2004-11-09 | Chicago Bridge & Iron Company | Claricone sludge level control system |
US7527726B2 (en) * | 2006-01-25 | 2009-05-05 | Q'max Solutions Inc. | Fluid treatment apparatus |
US7637379B2 (en) * | 2006-12-07 | 2009-12-29 | Council Of Scientific & Industrial Research | Circular secondary clarifier for wastewater treatment and an improved solids-liquid separation process thereof |
CA2629593A1 (en) * | 2008-04-11 | 2009-10-11 | James Michael Dunbar | Feedback control scheme for optimizing dewatering processes |
-
2008
- 2008-12-24 FR FR0807445A patent/FR2940270B1/en active Active
-
2009
- 2009-12-23 RU RU2011130809/05A patent/RU2501742C2/en not_active IP Right Cessation
- 2009-12-23 WO PCT/IB2009/055928 patent/WO2010073222A1/en active Application Filing
- 2009-12-23 CA CA2750849A patent/CA2750849C/en active Active
- 2009-12-23 ES ES09801559T patent/ES2733877T3/en active Active
- 2009-12-23 CN CN200980152285.8A patent/CN102264445B/en active Active
- 2009-12-23 BR BRPI0923619A patent/BRPI0923619A2/en not_active Application Discontinuation
- 2009-12-23 PT PT09801559T patent/PT2370194T/en unknown
- 2009-12-23 US US13/141,773 patent/US9011677B2/en active Active
- 2009-12-23 EP EP09801559.7A patent/EP2370194B1/en active Active
Non-Patent Citations (1)
Title |
---|
None * |
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US20110272346A1 (en) | 2011-11-10 |
CN102264445A (en) | 2011-11-30 |
RU2011130809A (en) | 2013-01-27 |
RU2501742C2 (en) | 2013-12-20 |
CA2750849C (en) | 2017-04-18 |
US9011677B2 (en) | 2015-04-21 |
ES2733877T3 (en) | 2019-12-03 |
CA2750849A1 (en) | 2010-07-01 |
BRPI0923619A2 (en) | 2016-01-12 |
EP2370194A1 (en) | 2011-10-05 |
WO2010073222A1 (en) | 2010-07-01 |
PT2370194T (en) | 2019-07-16 |
FR2940270A1 (en) | 2010-06-25 |
CN102264445B (en) | 2015-08-05 |
FR2940270B1 (en) | 2012-07-27 |
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